Method to tailor zeolite silica-to-alumina ratio

ABSTRACT

The present disclosure is directed to a method of manufacture of zeolite. A sol-gel formulation includes a water-soluble fraction of ODSO as an additional component. The resulting products include zeolite with increased SAR relative to comparable sol-gel formulations without ODSO as a precursor. In addition, the SAR is increased by increasing the ODSO content during synthesis. In additional embodiments, zeolite yield is also increased.

FIELD OF THE DISCLOSURE

The present disclosure relates to methods of making zeolites.

BACKGROUND OF THE DISCLOSURE Zeolites

Zeolites are crystalline solids possessing well-defined structures and uniform pore sizes that can be measured in angstroms (Å). Typically, zeolites comprise framework atoms such as silicon, aluminum and oxygen arranged as silica and alumina tetrahedra. Zeolites are generally hydrated aluminum silicates that can be made or selected with a controlled porosity and other characteristics, and typically contain cations, water and/or other molecules located in the porous network. Hundreds of natural and synthetic zeolite framework types exist with a wide range of applications. Numerous zeolites occur naturally and are extensively mined, whereas a wealth of interdependent research has resulted in an abundance of synthetic zeolites of different structures and compositions. The unique properties of zeolites and the ability to tailor zeolites for specific applications has resulted in the extensive use of zeolites in industry as catalysts, molecular sieves, adsorbents, ion exchange materials and for the separation of gases. Certain types of zeolites find application in various processes in petroleum refineries and many other applications. The zeolite pores can form sites for catalytic reactions, and can also form channels that are selective for the passage of certain compounds and/or isomers to the exclusion of others.

Aluminosilicate zeolites are typically synthesized via hydrothermal means from which zeolite crystals precipitate from a gel, using water as a solvent. The aluminosilicate zeolite comprises repeating tetrahedral unit cells as its framework comprising silicon, aluminum and oxygen. When trivalent Al substitutes for tetrahedral silica in the framework a negative charge is induced that is counter-balanced by a cation, typically an alkali metal such as Na⁺. In order for the zeolite to exhibit acidity the sodium cation should be replaced with a proton. The proton associated with counter-balancing the negative charge derived from the framework aluminum results in a Brønsted acid site. Lewis acidity typically results from extra-framework aluminum.

Hence, the number of acid sites correlates to a decreased Si/Al ratio (if protons are associated with the cation sites). The intrinsic acidity can be linked to the population of acid sites, with weakening Brønsted sites observed when the influence of proton crowding is elevated.

Therefore, controlling the acidity of the zeolite is a critical factor when considering its design for specific applications. Changes to the silica-to-alumina (SAR) ratio can result in unsuitable product outcomes. Fine tuning of the acidity functionality allows control over a critical parameter that may optimize product outcome and maximize profitability. Current methods to fine tune the acid functionality during synthesis include adjusting the ratios of the silica and alumina source. Also, it is common to use post modification methods to change silica-alumina ratio of zeolites, which adds additional steps and therefore increases of the manufacturing process cost.

ODSO

Within a typical refinery, there are by-product streams that must be treated or otherwise disposed of. The mercaptan oxidation process, commonly referred to as the MEROX process, has long been employed for the removal of the generally foul smelling mercaptans found in many hydrocarbon streams and was introduced in the refining industry over fifty years ago. Because of regulatory requirements for the reduction of the sulfur content of fuels for environmental reasons, refineries have been, and continue to be faced with the disposal of large volumes of sulfur-containing by-products. Disulfide oil (DSO) compounds are produced as a by-product of the MEROX process, in which the mercaptans are removed from any of a variety of petroleum streams including liquefied petroleum gas, naphtha, and other hydrocarbon fractions. It is commonly referred to as a ‘sweetening process’ because it removes the sour or foul smelling mercaptans present in crude petroleum. The term “DSO” is used for convenience in this description and in the claims, and will be understood to include the mixture of disulfide oils produced as by-products of the mercaptan oxidation process. Examples of DSO include dimethyldisulfide, diethyldisulfide, and methylethyldisulfide.

The by-product DSO compounds produced by the MEROX unit can be processed and/or disposed of during the operation of various other refinery units. For example, DSO can be added to the fuel oil pool at the expense of a resulting higher sulfur content of the pool. DSO can be processed in a hydrotreating/hydrocracking unit at the expense of higher hydrogen consumption. DSO also has an unpleasant foul or sour smell, which is somewhat less prevalent because of its relatively lower vapor pressure at ambient temperature; however, problems exist in the handling of this oil.

Commonly owned U.S. Pat. No. 10,807,947 which is incorporated by reference herein in its entirety discloses a controlled catalytic oxidation of MEROX process by-products DSO. The resulting oxidized material is referred to as oxidized disulfide oil (ODSO). As disclosed in U.S. Pat. No. 10,807,947, the by-product DSO compounds from the mercaptan oxidation process can be oxidized, preferably in the presence of a catalyst. The oxidation reaction products constitute an abundant source of ODSO compounds, sulfoxides, sulfonates, sulfinates and sulfones.

The ODSO stream so-produced contains ODSO compounds as disclosed in U.S. Pat. Nos. 10,781,168 and 11,111,212 as compositions (such as a solvent), in U.S. Pat. No. 10,793,782 as an aromatics extraction solvent, and in U.S. Pat. No. 10,927,318 as a lubricity additive, all of which are incorporated by reference herein in their entireties. In the event that a refiner has produced or has on hand an amount of DSO compounds that is in excess of foreseeable needs for these or other uses, the refiner may wish to dispose of the DSO compounds in order to clear a storage vessel and/or eliminate the product from inventory for tax reasons.

Thus, there is a clear and long-standing need to provide an efficient and economical process for the treatment of the large volumes of DSO by-products and their derivatives to effect and modify their properties in order to facilitate and simplify their environmentally acceptable disposal, and to utilize the modified products in an economically and environmentally friendly manner, and thereby enhance the value of this class of by-products to the refiner.

Despite the known ways to produce zeolites, there remains a need in the art for improved methods to produce zeolite materials, in particular using DSO by-products in an economically and environmentally friendly manner. It is in regard to these and other problems in the art that the present disclosure is directed to provide a technical solution for an effective method of tailoring the zeolite SAR.

SUMMARY OF THE DISCLOSURE

A method for the preparation of zeolite is provided. The method comprises: forming a homogeneous aqueous mixture of a silica source, an aluminum source, an alkali metal source, an optional structure directing agent, water and water-soluble oxidized disulfide oil (ODSO); and heating the homogeneous aqueous mixture under conditions and for a time effective to form a crystalline zeolite as precipitate suspended in a supernatant, wherein the zeolite is characterized by a silica-to-alumina ratio that is greater than that of a comparative material, and wherein the comparative material is formed of approximately equivalent composition of components except for water instead of the added ODSO, and under approximately equivalent conditions and time.

In certain embodiments, an increase in a sub-ratio of water-soluble ODSO to water effects an increase in the silica-to-alumina ratio. In certain embodiments, the zeolite is characterized by a zeolite yield, and wherein the zeolite yield is greater than that of the comparative material. In certain embodiments, an increase in a sub-ratio of water-soluble ODSO to water effects an increase in the zeolite yield. In certain embodiments, the homogeneous aqueous mixture has a pH in the range of about 9-14, and wherein an increase in a sub-ratio of water-soluble ODSO to water effects a decrease in pH. In certain embodiments, the alkali metal source is sodium and the mass ratio of ODSO to sodium is in the range of about 0.1-10.

In certain embodiments, a method for synthesis of a first zeolite material and a second zeolite material is provided, comprising: forming a first homogeneous aqueous mixture at a first ratio of a silica source, an aluminum source, an alkali metal source, water, an optional a structure directing agent, and water-soluble oxidized disulfide oil (ODSO); heating the first homogeneous aqueous mixture under conditions and for a time effective to form a first crystalline zeolite as a first precipitate suspended in a supernatant, wherein the first zeolite material is characterized by a first silica-to-alumina ratio; forming a second homogeneous aqueous mixture at a second ratio of a silica source, an aluminum source, an alkali metal source, water, an optional a structure directing agent, and water-soluble ODSO, wherein the second ratio is approximately the same as the first ratio except for a ratio of water and water-soluble ODSO in the solution, wherein an amount of ODSO in the second homogeneous aqueous mixture is greater than an amount of ODSO in the first homogeneous aqueous mixture; heating the second homogeneous aqueous mixture approximately equivalent conditions and time as compared to the heating of the first homogeneous aqueous mixture to form a second crystalline zeolite as a second precipitate suspended in a supernatant, wherein the second zeolite material is characterized by a second silica-to-alumina ratio, and wherein the second silica-to-alumina ratio is greater than the first silica-to-alumina ratio. In certain embodiments, the first zeolite material and the second zeolite material zeolite are characterized by a first zeolite yield and a second zeolite yield, and wherein the second zeolite yield is greater than the first zeolite yield.

In certain embodiments, the ODSO is derived from oxidation of disulfide oil compounds present in an effluent refinery hydrocarbon stream recovered following catalytic oxidation of mercaptans present in a mercaptan-containing hydrocarbon stream. In certain embodiments, the ODSO compounds have 3 or more oxygen atoms and include one or more compounds selected from the group consisting of (R—SOO—SO—R′), (R—SOO—SOO—R′), (R—SO—SOO—OH), (R—SOO—SOO—OH), (R—SOO—SO—OH), (X—SO—OR) and (X—SOO—OR), wherein R and R′ are alkyl or aryl groups comprising 1-10 carbon atoms and wherein X denotes esters and is (R—SO) or (R—SOO). In certain embodiments, the ODSO compounds have 3 or more oxygen atoms and include two or more compounds selected from the group consisting of (R—SOO—SO—R′), (R—SOO—SOO—R′), (R—SO—SOO—OH), (R—SOO—SOO—OH), (R—SOO—SO—OH), (X—SO—OR) and (X—SOO—OR), wherein R and R′ are alkyl or aryl groups comprising 1-10 carbon atoms and wherein X denotes esters and is (R—SO) or (R—SOO). In certain embodiments, the ODSO compounds have 3 or more oxygen atoms and include one or more compounds selected from the group consisting of (R—SOO—SO—R′), (R—SOO—SOO—R′), (R—SO—SOO—OH), (R—SOO—SOO—OH), (R—SO—SO—OH), (R—SOO—SO—OH), wherein R and R′ are alkyl or aryl groups comprising 1-10 carbon atoms.

Any combinations of the various embodiments and implementations disclosed herein can be used. These and other aspects and features can be appreciated from the following description of certain embodiments and the accompanying drawings and claims.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a simplified schematic diagram of a generalized version of a conventional mercaptan oxidation or MEROX process for the liquid-liquid extraction of a mercaptan containing hydrocarbon stream.

FIG. 2 is a simplified schematic diagram of a generalized version of an enhanced mercaptan oxidation or E-MEROX process.

FIG. 3A is the experimental ¹H-NMR spectrum of the polar, water-soluble ODSO fraction used in an example herein.

FIG. 3B is the experimental ¹³C-DEPT-135-NMR spectrum of the polar, water-soluble ODSO fraction used in an example herein.

DETAILED DESCRIPTION OF CERTAIN EMBODIMENTS OF THE DISCLOSURE

The present disclosure is directed to a method of manufacture of zeolites. A sol-gel formulation includes a water-soluble fraction of ODSO as an additional component. The resulting products include zeolite with increased SAR relative to comparable sol-gel formulations without ODSO. In certain embodiments, the SAR can be tailored by adjusting the amount of ODSO component in the sol-gel formulation.

In certain embodiments the overall zeolite yield is increased using ODSO components as an additional component compared with an equivalent water-only zeolite synthesis. For example, inclusion of ODSO components in the syntheses herein:

-   -   increases the overall zeolite yield by at least about 1-80,         1-75, 1-70, 1-55, 1-50, 5-80, 5-75, 5-70, 5-55 or 5-50 mass %         compared with an equivalent water-only synthesis for MFI         zeolite;     -   increases the overall zeolite yield by at least about 1-80,         1-75, 1-55, 1-25, 1-15, 5-80, 5-75, 5-55, 5-25 or 5-15 mass %         compared with an equivalent water-only synthesis for BEA         zeolite; and     -   increases the overall zeolite yield by at least about 0.5-15,         0.5-12, 0.5-10, 1-15, 1-12 or 1-10 mass % compared with an         equivalent water-only synthesis for zeolite Y.

In certain embodiments, the SAR and/or the zeolite yield is increased, and zeolite having the same general zeolite framework as the equivalent water-only synthesis is produced. In certain embodiments, the SAR and/or the zeolite yield is increased, and zeolite having the same general zeolite framework as the equivalent water-only synthesis is produced along with one or more other types of zeolites and/or amorphous silica-alumina. In certain embodiments, the SAR and/or the zeolite yield is increased, and zeolite having a different general zeolite framework as the equivalent water-only synthesis is produced.

In conventional synthesis of zeolites, water is used as an aqueous medium and as a solvent. In the embodiments of the present disclosure, an effective amount of water-soluble ODSO compounds is added within a homogeneous aqueous mixture. In certain embodiments, the ODSO is derived from a sulfur-containing refinery waste stream of disulfide oil and is used as a component for the synthesis of zeolites having increased SAR as compared to an equivalent synthesis in the absence of ODSO.

The present disclosure is applicable to various types of zeolites that are synthesized hydrothermally, which can benefit from inclusion of ODSO components as described herein in the synthesis. Suitable zeolitic materials include those identified by the International Zeolite Association, including those with the identifiers ABW, ACO, AEI, AEL, AEN, AET, AFG, AFI, AFN, AFO, AFR, AFS, AFT, AFV, AFX, AFY, AHT, ANA, ANO, APC, APD, AST, ASV, ATN, ATO, ATS, ATT, ATV, AVE, AVL, AWO, AWW, BCT, BEC, BIK, BOF, BOG, BOZ, BPH, BRE, BSV, CAN, CAS, CDO, CFI, CGF, CGS, CHA, -CHI, -CLO, CON, CSV, CZP, DAC, DDR, DFO, DFT, DOH, DON, EAB, EDI, EEI, EMT, EON, EPI, ERI, ESV, ETL, ETR, ETV, EUO, EWO, EWS, EZT, FAR, FAU, FER, FRA, GIS, GIU, GME, GON, GOO, HEU, IFO, IFR, -IFT, -IFU, IFW, IFY, IHW, IMF, IRN, IRR, -IRY, ISV, ITE, ITG, ITH, ITR, ITT, -ITV, ITW, IWR, IWS, IWV, IWW, JBW, JNT, JOZ, JRY, JSN, JSR, JST, JSW, KFI, LAU, LEV, LIO, -LIT, LOS, LOV, LTA, LTF, LTJ, LTL, LTN, MAR, MAZ, MEI, MEL, MEP, MER, MFI, MFS, MON, MOR, MOZ, MRT, MSE, MSO, MTF, MTN, MTT, MTW, MVY, MWF, MWW, NAB, NAT, NES, NON, NPO, NPT, NSI, OBW, OFF, OKO, OSI, OSO, OWE, -PAR, PAU, PCR, PHI, PON, POR, POS, PSI, PTO, PTT, PTY, PUN, PWN, PWO, PWW, RHO, -RON, RRO, RSN, RTE, RTH, RUT, RWR, RWY, SAF, SAO, SAS, SAT, SAV, SBE, SBN, SBS, SBT, SEW, SFE, SFF, SFG, SFH, SFN, SFO, SFS, SFW, SGT, SIV, SOD, SOF, SOR, SOS, SOV, SSF, SSY, STF, STI, STT, STW, -SVR, SVV, SWY, -SYT, SZR, TER, THO, TOL, TON, TSC, TUN, UEI, UFI, UOS, UOV, UOZ, USI, UTL, UWY, VET, VFI, VNI, VSV, WEI, -WEN, YFI, YUG, ZON, *BEA, *CTH, *-EWT, *-ITN, *MRE, *PCS, *SFV, *-SSO, *STO, *-SVY, *UOE. For example, certain known zeolites used in the petroleum refining industry include but are not limited to mordenite, ZSM-5, ZSM-11, ZSM-12, ZSM-22, ZSM-23, ZSM-35, beta-type (*BEA), Y, USY, and MCM zeolites such as MCM-41 and MCM-48. For example, these can be (FAU) framework, which includes USY, having a micropore size related to the 12-member ring when viewed along the [111] direction of 7.4×7.4 Å; (MFI) framework, which includes ZSM-5, having a micropore size related to the 10-member rings when viewed along the [100] and [010] directions of 5.5×5.1 Å and 5.6×5.3 Å, respectively; (MEL) framework, which includes ZSM-11, having a micropore size related to the 10-member ring when viewed along the [100] direction of 5.4×5.3 Å; (MTW) framework, which includes ZSM-12, having a micropore size related to the 12-member ring when viewed along the [010] direction of 5.6×6.0 Å; (TON) framework, which includes ZSM-12, having a micropore size related to the 10-member ring when viewed along the [001] direction of 4.6×5.7 Å; (MTT) framework, which includes ZSM-23, having a micropore size related to the 10-member ring when viewed along the [001] direction of 4.5×5.2 Å; (FER) framework, which includes ZSM-35, having a micropore size related to the 10-member ring and 8-member ring when viewed along the [001] and [010] directions of 4.2×5.4 Å and 3.5×4.8 Å, respectively; (MOR) framework, which includes mordenite zeolites, having a micropore size related to the 12-member ring and 8-member ring when viewed along the [001] and [001] directions of 6.5×7.0 Å and 2.6×5.7 Å, respectively; and (*BEA) framework, which includes zeolite beta polymorph A, having a micropore size related to the 12-member rings when viewed along the [100] and [001] directions of 6.6×6.7 Å and 5.6×5.6 Å, respectively.

Synthesis Steps

Methods for the preparation of zeolites of various types are provided. Effective amounts and proportions of precursors and reagents are formed as a homogeneous aqueous mixture, including a water source, an aluminum source, a silica source, an alkali metal source, and an optional structure directing agent. In the place of a certain amount of water, an effective amount of water-soluble ODSO is used as an additional component. The components are mixed for an effective time and under conditions suitable to form the homogeneous aqueous mixture. The chronological sequence of mixing can vary, with the objective being a highly homogenous distribution of the components in an aqueous mixture. The homogeneous aqueous mixture is heated under conditions and for a time effective to form a precipitate (product) suspended in a supernatant (mother liquor). The precipitate is recovered, for example by filtration, washing and drying. The eventual framework of the as-made zeolites depend on various factors including but not limited to the time and/or temperature of hydrothermal reaction; selected structure directing agents (if any); selected seeds; and/or selected mineralizer. In certain embodiments, recovered precipitate is calcined at a suitable temperature, temperature ramp rate and for a suitable period of time. In certain embodiments, calcining is carried out to increase porosity. In certain embodiments, calcining is carried out to remove all or a portion of structure directing agent components that remain in the precipitate to realize porous zeolite.

An effective amount of water for the aqueous environment and as a solvent during the sol-gel process can be provided from one or more water sources, including utility water that is added to form the homogeneous aqueous mixture, a water-containing silica source such as colloidal silica, an aqueous mixture of an aluminum oxide source, an aqueous mixture of an alkali metal source, and/or an aqueous mixture of an optional structure directing agent. These mixture components are added with water to the reaction vessel prior to heating. Typically, water allows for adequate mixing to realize a more homogeneous distribution of the sol-gel components, which ultimately produces a more desirable product because each crystal is more closely matched in properties to the next crystal. Insufficient mixing could result in undesirable “pockets” of highly concentrated sol-gel components and this may lead to impurities in the form of different structural phases or morphologies. Water also determines the yield per volume. In the descriptions that follow, it is understood that water is a component of homogeneous aqueous mixtures from one or more of the sources of water.

In certain embodiments, the homogeneous aqueous mixture is formed by: providing a silica source; combining an aluminum oxide source, an alkali metal source and an optional structure directing agent; and combining water soluble ODSO. Alternatively, the water soluble ODSO is combined with the aluminum oxide source, the alkali metal source and the optional structure directing agent, and that mixture is combined with the silica source.

In certain embodiments, the homogeneous aqueous mixture is formed by: providing an aluminum oxide source, an alkali metal source and an optional structure directing agent as a mixture; combining a silica source; and combining water soluble ODSO. Alternatively, the water soluble ODSO is combined with the silica source, and that mixture is combined with the aluminum oxide source, the alkali metal source and the optional structure directing agent.

In certain embodiments, the homogeneous aqueous mixture is formed by: combining water soluble ODSO with a silica source to form a mixture; and that mixture is combined with an aluminum oxide source, an alkali metal source and an optional structure directing agent.

In certain embodiments, the homogeneous aqueous mixture is formed by: combining water soluble ODSO with an aluminum oxide source, an alkali metal source and an optional structure directing agent to form a mixture; and that mixture is combined with a silica source.

A homogeneous aqueous mixture of the aluminum source, silica source, alkali source, optional structure directing agent and ODSO is formed from any of the above chronological sequences of component addition. The homogeneous aqueous mixture heated under conditions and for a time effective to form a precipitate suspended in a supernatant, which is recovered, for example by filtration, washing and drying. In certain embodiments the recovered precipitate is calcined at a suitable temperature, temperature ramp rate and for a suitable period of time.

It is to be appreciated by those skilled in the art that in certain embodiments effective baseline compositional ratios for synthesis of zeolites as disclosed herein can be determined by empirical data, for instance summarized as phase boundary diagrams or other methodologies as is known in material synthesis. In certain embodiments, baseline compositional ratios and conditions are effective, in the absence of ODSO, for synthesis a zeolite with a certain SAR, and according to certain embodiments of the process herein, inclusion of an ODSO component results in increasing the SAR of the same type of zeolite. In certain embodiments, baseline compositional ratios and conditions are effective, in the absence of ODSO, for synthesis one type of zeolite, and according to certain embodiments of the process herein, inclusion of an ODSO component results in shifting the material type out of the phase boundary diagram, even at approximately equivalent ratios, to a different type of zeolite.

In certain embodiments, effective ratios of precursors and reagents for production of zeolites herein are within those known to produce templated aluminosilicate zeolites and can be determined by those of ordinary skill in the art. For example, effective amounts of silica and alumina precursors are provided to produce synthesized zeolite having a silica-to-alumina ratio (SAR) in the range of about 10-10000, 10-5000, 10-500, 10-100, 10-80, 50-10000, 50-5000, 50-1000, 50-500 or 50-100. In certain embodiments, baseline compositional ratios of the aqueous composition used to produce zeolites herein include (on a molar basis):

-   -   SiO₂/Al₂O₃: 10-1500     -   OH⁻/SiO₂: 0.05-3     -   R/SiO₂: 0-1.5     -   Alkali metal cation/SiO₂: 0.075-1.5     -   H₂O/SiO₂: 5-120     -   wherein R is the structure directing agent, and a level of 0         represents absence of the structure directing agent.         It is appreciated by those skilled in the art that these molar         composition ratios can be expressed on a mass basis. In certain         embodiments, an exemplary baseline compositional ratio effective         to produce *BEA zeolite is approximately 1 Al₂O₃:30 SiO₂:5.5         Na₂O:15 TEA:750 H₂O on a molar basis. In certain embodiments, an         exemplary baseline compositional ratio effective to produce FAU         zeolite is approximately 1 Al₂O₃:10 SiO₂:8 Na₂O:400 H₂O on a         molar basis. In certain embodiments, an exemplary baseline         compositional ratio effective to produce MFI zeolite is         approximately 1 Al₂O₃:100 SiO₂:13.4 Na₂O:20 TPA:2000 H₂O on a         molar basis.

As is known, different ratios of materials are used depending on the desired zeolite to be produced. In the embodiments herein, ratios of components in homogeneous aqueous mixtures including ODSO are referred to as “ODSO-enhanced compositional ratios.” In certain embodiments an ODSO-enhanced compositional ratio is one in which ODSO is included to replace an approximately equivalent mass of water in the homogeneous aqueous mixture, and wherein a cumulative amount of ODSO and water (ODSO+H₂O) is approximately equivalent to a mass of water that is effective to produce the same or another type of zeolite, or an amorphous material, in the absence of ODSO. In certain embodiments: a baseline compositional ratio of silica, aluminum, alkali metal, optional structure directing agent and water is known or determined to be is effective to produce the same or another type of zeolite, or an amorphous material, in the absence of ODSO; an ODSO-enhanced compositional ratio is approximately equivalent to the baseline compositional ratio except for the substitution of ODSO for water on a mass basis; and wherein the conditions and time of heating the ODSO-enhanced sol-gel is approximately equivalent to those that are effective to produce the same or another type of zeolite, or an amorphous material, in the absence of ODSO. For instance, in Comparative Example 1 herein, showing a composition that produces *BEA zeolite in the absence of ODSO, a baseline compositional ratio of Al₂O₃:SiO₂:Na₂O:TEA:H₂O is 1:30:5.5:15:750 on a molar basis, which can be expressed as a compositional ratio on a mass basis. In each of the Examples 1A, 1B, 1C, 1D and 1E, approximately equivalent ratios were used, except that an approximately equivalent mass of water was replaced with ODSO, and hence the ODSO-enhanced compositional ratio is approximately equivalent to the baseline ratio for the Comparative Example 1. For instance, in Comparative Example 2 herein, showing a composition that produces MFI zeolite in the absence of ODSO, a baseline compositional ratio of Al₂O₃:SiO₂:Na₂O:TPA:H₂O is 1:100:13.4:20:2000 on a molar basis, which can be expressed as a compositional ratio on a mass basis. In each of the Examples 2A and 2B, approximately equivalent molar ratios were used, except that an approximately equivalent mass of water was replaced with ODSO, and hence the ODSO-enhanced compositional ratio is approximately equivalent to the baseline ratio for the Comparative Example 2. For instance, in Comparative Example 3 herein, showing a composition that produces FAU zeolite in the absence of ODSO, a baseline compositional ratio of Al₂O₃:SiO₂:Na₂O:TPA:H₂O is 1:10:8:400 on a molar basis, which can be expressed as a compositional ratio on a mass basis. In each of the Examples 3A and 3B, approximately equivalent conditions, times and ratios were used, except that an approximately equivalent mass of water was replaced with ODSO, and hence the ODSO-enhanced compositional ratio is approximately equivalent to the baseline ratio for the Comparative Example 3.

The SAR levels in the synthesized zeolite depends on the type of zeolite; for instance: MFI zeolites including ZSM-5 have effective SAR (mol/mol) values in the synthesized zeolite in the range of about 20-1500, 20-1000, 20-500, 25-1500, 25-1000, 25-500, 50-1500, 50-1000, 50-500, 100-1500, 100-1000 or 100-500; *BEA zeolites, MOR zeolites or co-crystallized *BEA/MOR zeolites have effective SAR (mol/mol) values in the synthesized zeolite of greater than 10, in certain embodiments in the range of about 10-10000, 10-5000, 10-500, 10-100, 10-80, 50-10000, 50-5000, 50-1000, 50-500 or 50-100; zeolite Y has effective SAR (mol/mol) values in the synthesized zeolite in the range of about 3-6. In embodiments in which a structure directing agent is used, an effective amount includes a molar ratio (normalized to 1 mole of Al₂O₃) in the range of about 0.1-75, 0.1-50, 0.1-30, 0.1-20, 0.1-15, 1-75, 1-50, 1-30, 1-20, 1-15, 2.5-75, 2.5-50, 2.5-30, 5-75, 5-50 or 5-30.

The aluminum source can comprise, without limitation, one or more of aluminates, alumina, other zeolites, aluminum colloids, boehmites, pseudo-boehmites, aluminum salts such aluminum nitrate, aluminum sulfate and alumina chloride, aluminum hydroxides and alkoxides, aluminum wire and alumina gels. For example, suitable materials as aluminum sources include commercially available materials including for instance high purity aluminas (CERALOX commercially available from Sasol) and alumina hydrates (PURAL and CAPITAL commercially available from Sasol), boehmites (DISPERSAL and DISPAL commercially available from Sasol), and silica-alumina hydrates (SIRAL commercially available from Sasol) and the corresponding oxides (SIRALOX commercially available from Sasol).

The silica source can comprise, without limitation, one or more of silicates including sodium silicate (water glass), rice husk, fumed silica, precipitated silica, colloidal silica, silica gels, other zeolites, dealuminated zeolites, and silicon hydroxides and alkoxides. Silica sources resulting in a high relative yield are preferred. For instance, suitable materials as silica sources include fumed silica commercially available from Cabotand colloidal silica (LUDOX commercially available from Cabot).

In embodiments in which structure directing agents are used, they are selected to influence the target type of zeolite structure to be formed. Effective structure directing agents that can optionally be added include known or developed structure directing agents include one or more of quaternary ammonium ions, trialkylamines, dialkylamines, monoalkylamines, cyclic amines, alkylethanol amines, cyclic diamines, alkyl diamines, alkyl polyamines, and other templates including alcohols, ketones, morpholine and glycerol. For example, in embodiments in which the target zeolite structures are MFI, including ZSM-5, beta zeolite, or mordenite zeolite, suitable structure directing agents include but are not limited to one or more of quaternary ammonium cation compounds (including one or more of tetramethylammonium (TMA) cation compounds, tetraethylammonium (TEA) cation compounds, tetrapropylammonium (TPA) cation compounds, tetrabutylammonium (TBA) cation compounds, cetyltrimethylammonium (CTA) cation compounds; the cation can be paired with one or more of a hydroxide anion (for example, TPAOH or CTAOH), a bromide anion (for example, TPAB or CTAB), or an iodide anion. In embodiments in which the target zeolite structures are MFI zeolites, including ZSM-5, structure directing agents include but are not limited to one or more of: those identified above for MFI zeolites; bifunctional dicationic molecules containing a long aliphatic chain (for example C₂₂H₄₅—N⁺(CH₃)₂—C₆H₁₂-N⁺(CH₃)₂—C₆H₁₃, denoted C₂₂₋₆₋₆, C₂₂H₄₅—N⁺(CH₃)₂—C₆H₁₂—N⁺(CH₃)₂—C₃H₇, denoted C₂₂₋₆₋₃, or a poly(ethylene glycol)); dual-porogenic surfactants; silylated polyethylenimine polymers; amphiphilic organosilanes; or hydrophilic cationic polyelectroyltes/polymers such as poly(diallyldimethylammonium chloride) (PDADMAC). In embodiments in which the target zeolite structures are beta zeolites, structure directing agents include but are not limited to one or more of: those identified above for beta zeolite; 4,4′trimethylene bis(N-methyl N-benzyl-piperidinium) hydroxide; 1,2-diazabicyclo 2,2,2, octane (DABCO); dialkylbenzyl ammonium hydroxide; dimethyldiisopropylammonium hydroxide (DMDPOH); N,N-dimethyl-2,6-cis-dimethylpiperdinium hydroxide (DMPOH); N-ethyl-N,N-dimethylcyclohexanaminium hydroxide (EDMCHOH); N,N,N-trimethylcyclohexanaminium hydroxide (TMCHOH); N-isopropyl-N-methyl-pyrrolidinium (iProOH); N-isobutyl-N-methyl-pyrrolidinium (iButOH); N-isopentyl-N-methyl-pyrrolidinium (iPenOH); or any of the thousands of structure directing agents for producing zeolite beta can be used, as disclosed in Daeyaerta et al., “Machine-learning approach to the design of OSDAs for zeolite beta,” PNAS February, 116 (2019): 3413-3418. In embodiments in which the target zeolite structures are mordenite zeolite, structure directing agents include but are not limited to one or more of: those identified above for mordenite zeolite; mixed organic templates such as glycerol, ethylene glycol or polyethylene glycol; pyrrolidine-based mesoporogens; piperazine; 1,6-diaminohexane; diethylpiperidinium; or co-operative organic templates such as N,N,N-trimethyl-1,1-adamantammonium and 1,2-hexanediol.

The disclosed process for synthesizing zeolite herein can occur in the absence or presence of seed materials comprising zeolite structures of the same or similar crystalline framework structure as the target zeolite framework for production. For example: for MFI zeolites, suitable seed materials include ZSM-5 (MFI), ZSM-8 (MFI), ZSM-11 (MEL) and Silicalite-1 (MFI); for beta zeolites, other beta zeolites are used as seed materials; for mordenite zeolites, other mordenite zeolites are used as seed materials; for FAU zeolites, suitable seed materials are zeolite Y, zeolite X, USY zeolite, faujasite zeolite or small protozeolitic species (gels). Functions of the seeds can include, but are not limited to: supporting growth on the surface of the seed, that is, where crystallization does not undergo nucleation but rather crystal growth is directly on the surface of the seed; the parent gel and seed share common larger composite building units; the parent gel and seed share common smaller units, for instance 4 member rings; seeds that undergo partial dissolution to provide a surface for crystal growth of a zeolite; crystallization occurs through a “core-shell” mechanism with the seed acting as a core and the target material grows on the surface; and/or where the seeds partially dissolve providing essential building units that can orientate zeolite crystallization.

A hydroxide mineralizer is included as the hydroxide derived from the alkali metal source from the Periodic Table IUPAC Group 1 alkaline metals (and/or from the hydroxide of any hydroxide-containing structure directing agent). For example, these are selected from the group consisting of NaOH, KOH, RbOH, LiOH, CsOH and combinations thereof. In certain embodiments a Na-based hydroxide mineralizer is selected. Note that the alkali metal source is provide as a hydroxide, but in embodiments herein where the ratio is expressed based on the mass of the alkali, it is the metal itself. For instance, when the alkali is NaOH, the ODSO/Na ratio is determined by dividing the mass of the ODSO by the mass of the Na portion of NaOH, that is, about 57.5% of the NaOH mass. In certain embodiments the basic components from the hydroxide mineralizer source are provided in effective amounts so as to maintain the homogeneous mixture at a pH level of greater than or equal to about 9, for example in the range of about 9-14, 9-13, 10-14, 10-13, 11-14 or 11-13. It is appreciated that the overall pH is influenced by anions from the hydroxide mineralizer source, and in certain embodiments anions from other sources such as from an alumina source or a silica source. In certain embodiments hydroxide anions are provided as the mineralizer from an alkali metal source and a structure directing agent. In the process herein, the pH is reduced by the presence of ODSO, therefore, the quantity of the basic compound from one or more of the aforementioned sources can be adjusted accordingly to attain the requisite pH.

The mixing steps typically occur at ambient temperature and pressure (for instance about 20° C. and about 1 standard atmosphere), for a time is sufficient to realize a homogeneous distribution of the components. In certain embodiments the sol-gel can be aged before being subjected to subsequent hydrothermal treatment, for example for a period of about 0-48, 0-24, 0-5, 0.5-24 or 0.5-5 hours. Hydrothermal treatment is then carried out at a temperature in the range of about 100-200, 100-180, 100-160, 120-200, 120-180, 120-160 or 140-200° C. and at atmospheric or autogenous pressure (from the sol-gel or from the sol-gel plus an addition of a gas purge into the vessel prior to heating), and for a time period within the range of about 0.1-7, 0.2-7, 0.1-6, 0.2-6, 0.1-5 or 0.2-5 days, to ensure crystallization and formation of a zeolite gel. As is known, these time periods and temperatures can vary depending on the desired zeolite framework to be produced.

The products are washed, for example with water at a suitable quantity, for example at about twice the volume of the sol-gel solution. The wash can be at a temperature of from about 20-80° C. at atmospheric, vacuum or under pressure. The wash can continue until the pH of the filtrate approaches about 7-9. The solids are recovered by filtration, for instance, using known techniques such as centrifugation, gravity, vacuum filtration, filter press, or rotary drums, and dried, for example at a temperature of up to about 110 or 150° C.

The conditions for calcination in embodiments in which it is carried out can include temperatures in the range of about 450-700, 450-600, 500-700 or 500-600° C., atmospheric pressure, and a time period of about 3-24, 3-18, 6-24 or 6-18 hours. Calcining can occur with ramp rates in the range of from about 0.1-10, 0.1-5, 0.1-3, 1-10, 1-5 or 1-3° C. per minute. In certain embodiments calcination can have a first step ramping to a temperature of between about 100-150° C. with a holding time of from about 2-24 hours (at ramp rates of from about 0.1-5, 0.1-3, 1-5 or 1-3° C. per min) before increasing to a higher temperature with a final holding time in the range of about 2-24 hours.

ODSO

Example embodiments of the present disclosure are directed to one or more ODSO compounds that are used as additional components in a homogeneous aqueous mixture for zeolite synthesis. The additional components can be a mixture that comprises two or more ODSO compounds. In the description herein, the terms “oxidized disulfide oil”, “ODSO”, “ODSO mixture” and “ODSO compound(s)” may be used interchangeably for convenience. As used herein, the abbreviations of oxidized disulfide oils (“ODSO”) and disulfide oils (“DSO”) will be understood to refer to the singular and plural forms, which may also appear as “DSO compounds” and “ODSO compounds,” and each form may be used interchangeably. In certain instances, a singular ODSO compound may also be referenced.

In the process herein, an effective amount of one or more ODSO compounds are used in the synthesis of zeolite. In certain embodiments an effective amount can be based on an amount that attains a desired pH range. In certain embodiments an effective amount can be approximately equivalent to a reduction in the amount of water that is used in the homogeneous aqueous mixture compared to synthesis without ODSO. In certain embodiments an effective amount can be based on a ratio of ODSO to alkali metal. In certain embodiments a ratio of ODSO to alkali metal represents the amount of ODSO relative to the amount of the selected alkali metal on a mass/mass basis or a molar/molar basis. For example, if sodium is used the ratio is expressed as ODSO/Na on a mass/mass basis or a molar/molar basis. In certain embodiments, the effective amount of ODSO is that which results in a pH level of greater than or equal to about 9, for example in the range of about 9-14, 9-13, 10-15, 10-14, 10-13 or 11-14 in the intermediate suspension of the precipitate suspended in the supernatant. In certain embodiments, the effective amount of ODSO can be relative to the quantity of basic groups in the sol gel, such as OH⁻, to attain a desired pH range, with basic group contributions from the alkali metal source; such a ratio can be expressed on a molar basis. In certain embodiments, the effective amount of ODSO is that which results in the synthesis of zeolite is an ODSO/Na ratio (wt./wt.) in the range of about 0.1-10, 0.1-9, 0.1-8, 0.1-7, 0.1-6, 0.1-5, 0.1-4, 0.1-3, 0.1-2, 0.1-1, 1-10, 1-9, 1-8, 1-7, 1-6, 1-5, 1-4, 1-3, 1-2, 2-10, 2-9, 2-8, 2-7, 2-6, 2-5, 2-4 or 2-3. It is noted that various factors can contribute to quantity of ODSO, including the type of zeolite formed, the ratios of other components, and the amount of mineralizer. For example, in processes in which the SAR is increased in MFI zeolite, examples herein were carried out at ODSO/Na ratios of about 5.3 and 8.6, with SAR increases of about 44% and 53% and yield increases of about 49% and 70%, respectively, compared to an approximately equivalent ratio of sol-gel precursors in a comparative example without ODSO. For example, in processes in which the SAR is increased in FAU zeolite, examples herein were carried out at ODSO/Na ratios between about 0.92 and 1.85, with SAR increases of about 9% and yield increases of about 4%, compared to an approximately equivalent ratio of sol-gel precursors in a comparative example without ODSO For example, in processes in which the SAR is increased in *BEA zeolite, MOR zeolite, or both *BEA MOR zeolite, examples herein were carried with ODSO/Na ratios between about 1.3 and 8, with SAR increases of between about 9% and 71% and yield increases of between about 14% and 74%, respectively, compared to an approximately equivalent ratio of sol-gel precursors in a comparative example without ODSO.

In certain embodiments, the ODSO compounds used as the additional component used herein is derived from controlled catalytic oxidation of disulfide oils from mercaptan oxidation processes. The effluents from controlled catalytic oxidation of disulfide oils from mercaptan oxidation processes includes ODSO compounds and in certain embodiments DSO compounds that were unconverted in the oxidation process. In certain embodiments this effluent contains water-soluble compounds and water-insoluble compounds. The effluent contains at least one ODSO compound, or a mixture of two or more ODSO compounds, selected from the group consisting of compounds having the general formula (R—SO—S—R′), (R—SOO—S—R′), (R—SOO—SO—R′), (R—SOO—SOO—R′), (R—SO—SO—R′), (R—SO—SOO—OH), (R—SOO—SOO—OH), (R—SO—SO—OH), (R—SOO—SO—OH), (X—SO—OR) and (X—SOO—OR). In certain embodiments, in the above formulae R and R′ are alkyl or aryl groups comprising 1-10 carbon atoms. Further, X denotes esters and is (R—SO) or (R—SOO), with R as defined above. It will be understood that since the source of the DSO is a refinery feedstream, the R and X substituents vary, e.g., methyl and ethyl subgroups, and the number of sulfur atoms, S, in the as-received feedstream to oxidation can extend to 3, for example, trisulfide compounds.

In certain embodiments the water-soluble compounds and water-insoluble compounds are separated from one another, and a component used herein for zeolite synthesis comprises all or a portion of the water-soluble compounds separated from the total effluents from oxidation of disulfide oils from mercaptan oxidation processes. For example, the different phases can be separated by decantation or partitioning with a separating funnel, separation drum, by decantation, or any other known apparatus or process for separating two immiscible phases from one another. In certain embodiments, the water-soluble and water-insoluble components can be separated by distillation as they have different boiling point ranges. It is understood that there will be crossover of the water-soluble and water-insoluble components in each fraction due to solubility of components, typically in the ppmw range (for instance, about 1-10,000, 1-1,000, 1-500 or 1-200 ppmw). In certain embodiments, contaminants from each phase can be removed, for example by stripping or adsorption.

In certain embodiments a component used herein for zeolite synthesis comprises, consists of or consists essentially of at least one water-soluble ODSO compound having 3 or more oxygen atoms that is selected from the group consisting of compounds having the general formula (R—SOO—SO—R′), (R—SOO—SOO—R′), (R—SO—SOO—OH), (R—SOO—SOO—OH), (R—SOO—SO—OH), (X—SO—OR) and (X—SOO—OR). In certain embodiments a component used herein for zeolite synthesis comprises, consists of or consists essentially of a mixture or two or more water-soluble ODSO compounds having 3 or more oxygen atoms, that is selected from the group consisting of compounds having the general formula (R—SOO—SO—R′), (R—SOO—SOO—R′), (R—SO—SOO—OH), (R—SOO—SOO—OH), (R—SOO—SO—OH), (X—SO—OR) and (X—SOO—OR). In certain embodiments a component used herein for zeolite synthesis comprises, consists of or consists essentially of ODSO compounds selected from the group consisting of (R—SOO—SO—R′), (R—SOO—SOO—R′), (R—SO—SOO—OH), (R—SOO—SOO—OH), (R—SO—SO—OH), (R—SOO—SO—OH), and mixtures thereof. In certain embodiments, in the above formulae R and R′ are alkyl or aryl groups comprising 1-10 carbon atoms. Further, X denotes esters and is (R—SO) or (R—SOO), with R as defined above. In certain embodiments, the R and R′ are methyl and/or ethyl groups. In certain embodiments, the ODSO compound(s) used herein a component for zeolite synthesis have 1 to 20 carbon atoms.

In certain embodiments, a component used herein for zeolite synthesis comprises, consists of or consists essentially of ODSO compounds having an average density greater than about 1.0 g/cc. In certain embodiments, a component used herein for zeolite synthesis comprises, consists of or consists essentially of ODSO compounds having an average boiling point greater than about 80° C. In certain embodiments, a component used herein for zeolite synthesis comprises, consists of or consists essentially of ODSO compounds having a dielectric constant that is less than or equal to 100 at 0° C.

Table 1 includes examples of polar water-soluble ODSO compounds that contain 3 or more oxygen atoms. In certain embodiments the identified ODSO compounds are obtained from a water-soluble fraction of the effluents from oxidation of DSO obtained from MEROX by-products. The ODSO compounds that contain 3 or more oxygen atoms are water-soluble over effectively all concentrations, for instance, with some minor amount of acceptable tolerance for carry over components from the effluent stream and in the water insoluble fraction with 2 oxygen atoms of no more than about 1, 3 or 5 mass percent.

In certain embodiments the ODSO compounds used as a precursor component comprise all or a portion of the ODSO compounds contained in an oxidation effluent stream that is obtained by controlled catalytic oxidation of MEROX process by-products, DSO compounds, as disclosed in U.S. Pat. Nos. 10,807,947 and 10,781,168 and as incorporated herein by reference above.

In some embodiments, the ODSO compounds used as a component for zeolite synthesis are derived from oxidized DSO compounds present in an effluent refinery hydrocarbon stream recovered following the catalytic oxidation of mercaptans present in the hydrocarbon stream. In some embodiments, the DSO compounds are oxidized in the presence of a catalyst.

As noted above, the designation “MEROX” originates from the function of the process itself, that is, the conversion of mercaptans by oxidation. The MEROX process in all of its applications is based on the ability of an organometallic catalyst in a basic environment, such as a caustic, to accelerate the oxidation of mercaptans to disulfides at near ambient temperatures and pressures. The overall reaction can be expressed as follows:

RSH+¼O₂→½RSSR+½H₂O   (1)

where R is a hydrocarbon chain that may be straight, branched, or cyclic, and the chains can be saturated or unsaturated. In most petroleum fractions, there will be a mixture of mercaptans so that the R can have 1, 2, 3 and up to 10 or more carbon atoms in the chain. This variable chain length is indicated by R and R′ in the reaction. The reaction is then written:

2R′SH+2RSH+O₂→2R′SSR+2H₂O   (2)

This reaction occurs spontaneously whenever any sour mercaptan-bearing distillate is exposed to atmospheric oxygen, but proceeds at a very slow rate. In addition, the catalyzed reaction (1) set forth above requires the presence of an alkali caustic solution, such as aqueous sodium hydroxide. The mercaptan oxidation proceeds at an economically practical rate at moderate refinery downstream temperatures.

The MEROX process can be conducted on both liquid streams and on combined gaseous and liquid streams. In the case of liquid streams, the mercaptans are converted directly to disulfides which remain in the product so that there is no reduction in total sulfur content of the effluent stream. The MEROX process typically utilizes a fixed bed reactor system for liquid streams and is normally employed with charge stocks having end points above 135° C. -150° C. Mercaptans are converted to disulfides in the fixed bed reactor system over a catalyst, for example, an activated charcoal impregnated with the MEROX reagent, and wetted with caustic solution. Air is injected into the hydrocarbon feedstream ahead of the reactor and in passing through the catalyst-impregnated bed, the mercaptans in the feed are oxidized to disulfides. The disulfides are substantially insoluble in the caustic and remain in the hydrocarbon phase. Post treatment is required to remove undesirable by-products resulting from known side reactions such as the neutralization of H₂S, the oxidation of phenolic compounds, entrained caustic, and others.

The vapor pressures of disulfides are relatively low compared to those of mercaptans, so that their presence is much less objectionable from the standpoint of odor; however, they are not environmentally acceptable due to their sulfur content and their disposal can be problematical.

In the case of mixed gas and liquid streams, extraction is applied to both phases of the hydrocarbon streams. The degree of completeness of the mercaptan extraction depends upon the solubility of the mercaptans in the alkaline solution, which is a function of the molecular weight of the individual mercaptans, the extent of the branching of the mercaptan molecules, the concentration of the caustic soda and the temperature of the system. Thereafter, the resulting DSO compounds are separated and the caustic solution is regenerated by oxidation with air in the presence of the catalyst and reused.

Referring to the attached drawings, FIG. 1 is a simplified schematic of a generalized version of a conventional MEROX process employing liquid-liquid extraction for removing sulfur compounds. A MEROX unit 1010, is provided for treating a mercaptan containing hydrocarbon stream 1001. In some embodiments, the mercaptan containing hydrocarbon stream 1001 is LPG, propane, butane, light naphtha, kerosene, jet fuel, or a mixture thereof. The process generally includes the steps of: introducing the hydrocarbon stream 1001 with a homogeneous catalyst into an extraction vessel 1005 containing a caustic solution 1002, in some embodiments, the catalyst is a homogeneous cobalt-based catalyst; passing the hydrocarbon catalyst stream in counter-current flow through the extraction section of the extraction 1005 vessel in which the extraction section includes one or more liquid-liquid contacting extraction decks or trays (not shown) for the catalyzed reaction with the circulating caustic solution to convert the mercaptans to water-soluble alkali metal alkane thiolate compounds; withdrawing a hydrocarbon product stream 1003 that is free or substantially free of mercaptans from the extraction vessel 1005, for instance, having no more than about 1000, 100, 10 or 1 ppmw mercaptans; recovering a combined spent caustic and alkali metal alkane thiolate stream 1004 from the extraction vessel 1005; subjecting the spent caustic and alkali metal alkane thiolate stream 1004 to catalyzed wet air oxidation in a reactor 1020 into which is introduced catalyst 1005 and air 1006 to provide the regenerated spent caustic 1008 and convert the alkali metal alkane thiolate compounds to disulfide oils; and recovering a by-product stream 1007 of DSO compounds and a minor proportion of other sulfides such as mono-sulfides and tri-sulfides. The effluents of the wet air oxidation step in the MEROX process can comprise a minor proportion of sulfides and a major proportion of disulfide oils. As is known to those skilled in the art, the composition of this effluent stream depends on the effectiveness of the MEROX process, and sulfides are assumed to be carried-over material. A variety of catalysts have been developed for the commercial practice of the process. The efficiency of the MEROX process is also a function of the amount of H₂S present in the stream. It is a common refinery practice to install a prewashing step for H₂S removal.

An enhanced MEROX process (“E-MEROX”) is a modified MEROX process where an additional step is added, in which DSO compounds are oxidized with an oxidant in the presence of a catalyst to produce a mixture of ODSO compounds. The by-product DSO compounds from the mercaptan oxidation process are oxidized, in some embodiments in the presence of a catalyst, and constitute an abundant source of ODSO compounds that are sulfoxides, sulfonates, sulfinates, sulfones and their corresponding di-sulfur mixtures. The disulfide oils having the general formula RSSR′ (wherein R and R′ can be the same or different and can have 1, 2, 3 and up to 10 or more carbon atoms) can be oxidized without a catalyst or in the presence of one or more catalysts to produce a mixture of ODSO compounds. The oxidant can be a liquid peroxide selected from the group consisting of alkyl hydroperoxides, aryl hydroperoxides, dialkyl peroxides, diaryl peroxides, peresters and hydrogen peroxide. The oxidant can also be a gas, including air, oxygen, ozone and oxides of nitrogen. If a catalyst is used in the oxidation of the disulfide oils having the general formula RSSR′ to produce the ODSO compounds, it can be a heterogeneous or homogeneous oxidation catalyst. The oxidation catalyst can be selected from one or more heterogeneous or homogeneous catalyst comprising metals from the IUPAC Group 4-12 of the Periodic Table, including Ti, V, Mn, Co, Fe, Cr, Cu, Zn, W and Mo. The catalyst can be a homogeneous water-soluble compound that is a transition metal containing an active species selected from the group consisting of Mo (VI), W (VI), V (V), Ti (IV), and their combination. In certain embodiments, suitable homogeneous catalysts include molybdenum naphthenate, sodium tungstate, molybdenum hexacarbonyl, tungsten hexacarbonyl, sodium tungstate and vanadium pentoxide. An exemplary catalyst for the controlled catalytic oxidation of MEROX process by-products DSO is sodium tungstate, Na₂WO₄·2H₂O. In certain embodiments, suitable heterogeneous catalysts include Ti, V, Mn, Co, Fe, Cr, W, Mo, and combinations thereof deposited on a support such as alumina, silica-alumina, silica, natural zeolites, synthetic zeolites, and combinations comprising one or more of the above supports.

The oxidation of DSO typically is carried out in an oxidation vessel selected from one or more of a fixed-bed reactor, an ebullated bed reactor, a slurry bed reactor, a moving bed reactor, a continuous stirred tank reactor, and a tubular reactor. The ODSO compounds produced in the E-MEROX process generally comprise two phases: a water-soluble phase and water-insoluble phase, and can be separated into the aqueous phase containing water-soluble ODSO compounds and a non-aqueous phase containing water-insoluble ODSO compounds. The E-MEROX process can be tuned depending on the desired ratio of water-soluble to water-insoluble compounds presented in the product ODSO mixture. Partial oxidation of DSO compounds results in a higher relative amount of water-insoluble ODSO compounds present in the ODSO product and a near or almost complete oxidation of DSO compounds results in a higher relative amount of water-soluble ODSO present in the ODSO product. Details of the ODSO compositions are discussed in the U.S. Pat. No. 10,781,168, which is incorporated herein by reference above.

FIG. 2 is a simplified schematic of an E-MEROX process that includes E-MEROX unit 1030. The MEROX unit 1010 unit operates similarly as in FIG. 1 , with similar references numbers representing similar units/feeds. In FIG. 2 , the effluent stream 1007 from the generalized MEROX unit of FIG. 1 is treated. It will be understood that the processing of the mercaptan containing hydrocarbon stream of FIG. 1 is illustrative only and that separate streams of the products, and combined or separate streams of other mixed and longer chain products can be the subject of the process for the recovery and oxidation of DSO to produce ODSO compounds, that is the E-MEROX process. In order to practice the E-MEROX process, apparatus are added to recover the by-product DSO compounds from the MEROX process. In addition, a suitable reactor 1035 add into which the DSO compounds are introduced in the presence of a catalyst 1032 and an oxidant 1034 and subjecting the DSO compounds to a catalytic oxidation step to produce the mixed stream 1036 of water and ODSO compounds. A separation vessel 1040 is provided to separate the by-product 1044 from the ODSO compounds 1042.

The oxidation to produce OSDO can be carried out in a suitable oxidation reaction vessel operating at a pressure in the range from about 1-30, 1-10 or 1-3 bars. The oxidation to produce OSDO can be carried out at a temperature in the range from about 20-300, 20-150, 20-90, 45-300, 15-150 or 45-90° C. The molar feed ratio of oxidizing agent-to-mono-sulfur can be in the range of from about 1:1 to 100:1, 1:1 to 30:1 or 1:1 to 4:1. The residence time in the reaction vessel can be in the range of from about 5-180, 5-90, 5-30, 15-180, 15-90 or 5-30 minutes. In certain embodiments, oxidation of DSO is carried out in an environment without added water as a reagent. The by-products stream 1044 generally comprises wastewater when hydrogen peroxide is used as the oxidant. Alternatively, when other organic peroxides are used as the oxidant, the by-products stream 1044 generally comprises the alcohol of the peroxide used. For example, if butyl peroxide is used as the oxidant, the by-product alcohol 1044 is butanol.

In certain embodiments water-soluble ODSO compounds are passed to a fractionation zone (not shown) for recovery following their separation from the wastewater fraction. The fractionation zone can include a distillation unit. In certain embodiments, the distillation unit can be a flash distillation unit with no theoretical plates in order to obtain distillation cuts with larger overlaps with each other or, alternatively, on other embodiments, the distillation unit can be a flash distillation unit with at least 15 theoretical plates in order to have effective separation between cuts. In certain embodiments, the distillation unit can operate at atmospheric pressure and at a temperature in the range of from 100° C. to 225° C. In other embodiments, the fractionation can be carried out continuously under vacuum conditions. In those embodiments, fractionation occurs at reduced pressures and at their respective boiling temperatures. For example, at 350 mbar and 10 mbar, the temperature ranges are from 80° C. to 194° C. and 11° C. to 98° C., respectively. Following fractionation, the wastewater is sent to the wastewater pool (not shown) for conventional treatment prior to its disposal. The wastewater by-product fraction can contain a small amount of water-insoluble ODSO compounds, for example, in the range of from 1 ppmw to 10,000 ppmw. The wastewater by-product fraction can contain a small amount of water-soluble ODSO compounds, for example, in the range of from 1 ppmw to 50,000 ppmw, or 100 ppmw to 50,000 ppmw. In embodiments where alcohol is the by-product alcohol, the alcohol can be recovered and sold as a commodity product or added to fuels like gasoline. The alcohol by-product fraction can contain a small amount of water-insoluble ODSO compounds, for example, in the range of from 1 ppmw to 10,000 ppmw. The alcohol by-product fraction can contain a small amount of water-soluble ODSO compounds, for example, in the range of from 100 ppmw to 50,000 ppmw.

EXAMPLES

The below examples and data are exemplary. It is to be understood that other ratios and types of aluminum sources, silica sources, bases and structure directing agents can be used as compared to the examples.

Reference Example: The ODSO mixture used in the Example below was produced as disclosed in U.S. Pat. No. 10,781,168, incorporated by reference above, and in particular the fraction referred to therein as Composition 2. Catalytic oxidation a hydrocarbon refinery feedstock having 98 mass percent of C1 and C2 disulfide oils was carried out. The oxidation of the DSO compounds was performed in batch mode under reflux at atmospheric pressure, that is, approximately 1.01 bar. The hydrogen peroxide oxidant was added at room temperature, that is, approximately 23° C. and produced an exothermic reaction. The molar ratio of oxidant-to-DSO compounds (calculated based upon mono-sulfur content) was 2.90. After the addition of the oxidant was complete, the reaction vessel temperature was set to reflux at 80° C. for approximately one hour after which the water soluble ODSO was produced (referred to as Composition 2 herein and in U.S. Pat. No. 10,781,168) and isolated after the removal of water. The catalyst used in the oxidation of the DSO compounds was sodium tungstate. The Composition 2, referred to herein as “the selected water soluble ODSO fraction,” was used. FIG. 3A is the experimental ¹H-NMR spectrum of the polar, water soluble ODSO mixture that is the selected water soluble ODSO fraction in the example herein. FIG. 3B is the experimental ¹³C-DEPT-135-NMR spectrum of the polar, water soluble ODSO mixture that is the selected water soluble ODSO fraction in the example herein. The selected water soluble ODSO fraction was mixed with a CD₃OD solvent and the spectrum was taken at 25° C. Methyl carbons have a positive intensity while methylene carbons exhibit a negative intensity. The peaks in the 48-50 ppm region belong to carbon signals of the CD₃OD solvent.

When comparing the experimental ¹³C-DEPT-135-NMR spectrum of FIG. 3B for the selected water soluble ODSO fraction with a saved database of predicted spectra, it was found that a combination of the predicted alkyl-sulfoxidesulfonate (R—SO—SOO—OH), alkyl-sulfonesulfonate (R—SOO—SOO—OH), alkyl-sulfoxidesulfinate (R—SO—SO—OH)and alkyl-sulfonesulfinate (R—SOO—SO—OH) most closely corresponded to the experimental spectrum. This suggests that alkyl-sulfoxidesulfonate (R—SO—SOO—OH), alkyl-sulfonesulfonate (R—SOO—SOO—OH), alkyl-sulfoxidesulfinate (R—SO—SO—OH) and alkyl-sulfonesulfinate (R—SOO—SO—OH) are major compounds in the selected water soluble ODSO fraction. It is clear from the NMR spectra shown in FIGS. 3A and 3B that the selected water soluble ODSO fraction comprises a mixture of ODSO compounds that form the ODSO composition used in the present examples.

Comparative Example 1: Precursors for synthesis of beta zeolite were provided in a comparative example, that is, in the absence of ODSO (ODSO/Na (g/g)=0), with a sol-gel SAR of about 30. Aluminum nitrate nonahydrate (0.6955 g) was weighed into a polytetrafluoroethylene (PTFE) liner (45 ml). Thereafter, 0.8144 g of a 50 wt. % sodium hydroxide solution and 5.0878 g of a 40 wt. % tetraethylammonium hydroxide (TEAOH) solution were added and the mixture stirred until the Al source dissolved. Next, distilled water (6.2386 g) was added and the mixture was kept under stirring. The silica source (4.1737 g, Ludox AS-40, SiO₂ content of 40 wt. %) was added and the mixture stirred until homogeneous. The PTFE liner was positioned within an autoclave and transferred to an oven and heated to a temperature of 140° C. whilst rotating the autoclave. The autoclave was kept at isothermal conditions for 6 days. Thereafter, the product was filtered and washed with distilled water before drying at 110° C. The dry mass was 1.1530 g. The inorganic content determined by thermogravimetric (TGA) analysis was 79.1%, which corresponds to a zeolite yield of 0.9119 g. The as-made product was determined by x-ray diffraction to be beta zeolite, which was calcined at 550° C. (1° C./min ramp rate) for 8 hours to realize porous beta zeolite. The SAR (mol/mol) of the calcined beta zeolite was determined to be 16.3 by inductively coupled plasma (ICP) spectroscopy.

Example 1A: ODSO as described in the Reference Example was added to replace an approximately equivalent amount of water (ODSO/Na (g/g)=1.33); other precursors are at ratios approximately equivalent to that in the Comparative Example 1, with a sol-gel SAR of about 30. Aluminum nitrate nonahydrate (0.6943 g) was weighed into a PTFE liner (45 ml). Thereafter, 0.8135 g of a 50 wt. % sodium hydroxide solution and 5.1063 g of a 40 wt. % TEAOH solution were added and the mixture stirred until the Al source dissolved. Next, distilled water (5.9149 g) and ODSO (0.3111 g) were added and the mixture was kept under stirring. The silica source (4.1695 g, Ludox AS-40, SiO₂ content of 40 wt. %) was added and the mixture stirred until homogeneous. The PTFE liner was positioned within an autoclave and transferred to an oven and heated to a temperature of 140° C. whilst rotating the autoclave. The autoclave was kept at isothermal conditions for 6 days. Thereafter, the product was filtered and washed with distilled water before drying at 110° C. The dry mass was 1.3452 g. The inorganic content determined by thermogravimetric (TGA) analysis was 77.1%, which corresponds to a zeolite yield of 1.0371 g. The as-made product was determined by x-ray diffraction to be beta zeolite, which was calcined at 550° C. (1° C./min ramp rate) for 8 hours to realize porous beta zeolite. The SAR (mol/mol) of the calcined beta zeolite was determined to be 17.8 by ICP spectroscopy.

Example 1B: ODSO as described in the Reference Example was added to replace an approximately equivalent amount of water (ODSO/Na (g/g)=2.66); other precursors are at ratios approximately equivalent to that in the Comparative Example 1, with a sol-gel SAR of about 30. Aluminum nitrate nonahydrate (0.6940 g) was weighed into a PTFE liner (45 ml). Thereafter, 0.8149 g of a 50 wt. % sodium hydroxide solution and 5.1046 g of a 40 wt. % TEAOH solution were added and the mixture stirred until the Al source dissolved. Next, distilled water (5.6084 g) and ODSO (0.6233 g) were added and the mixture was kept under stirring. The silica source (4.1712 g, Ludox AS-40, SiO₂ content of 40 wt. %) was added and the mixture stirred until homogeneous. The PTFE liner was positioned within an autoclave and transferred to an oven and heated to a temperature of 140° C. whilst rotating the autoclave. The autoclave was kept at isothermal conditions for 6 days. Thereafter, the product was filtered and washed with distilled water before drying at 110° C. The dry mass was 1.2196 g. The inorganic content determined by thermogravimetric (TGA) analysis was 85.9%, which corresponds to a zeolite yield of 1.0471 g. The as-made product was determined by x-ray diffraction to be mordenite zeolite, which was calcined at 550° C. (1° C./min ramp rate) for 8 hours to realize porous mordenite zeolite. The SAR (mol/mol) of the calcined mordenite zeolite was determined to be 18.6 by ICP spectroscopy.

Example 1C: ODSO as described in the Reference Example was added to replace an approximately equivalent amount of water (ODSO/Na (g/g)=3.99); other precursors are at ratios approximately equivalent to that in the Comparative Example 1, with a sol-gel SAR of about 30. Aluminum nitrate nonahydrate (0.6942 g) was weighed into a PTFE liner (45 ml). Thereafter, 0.8144 g of a 50 wt. % sodium hydroxide solution and 5.1047 g of a 40 wt. % TEAOH solution were added and the mixture stirred until the Al source dissolved. Next, distilled water (5.2990 g) and ODSO (0.9334 g) were added and the mixture was kept under stirring. The silica source (4.1705 g, Ludox AS-40, SiO₂ content of 40 wt. %) was added and the mixture stirred until homogeneous. The PTFE liner was positioned within an autoclave and transferred to an oven and heated to a temperature of 140° C. whilst rotating the autoclave. The autoclave was kept at isothermal conditions for 6 days. Thereafter, the product was filtered and washed with distilled water before drying at 110° C. The dry mass was 1.3032 g. The inorganic content determined by thermogravimetric (TGA) analysis was 85.8%, which corresponds to a zeolite yield of 1.1183 g. The as-made product was determined by x-ray diffraction to be mordenite zeolite, which was calcined at 550° C. (1° C./min ramp rate) for 8 hours to realize porous mordenite zeolite. The SAR (mol/mol) of the calcined mordenite zeolite was determined to be 20.2 by ICP spectroscopy.

Example 1D: ODSO as described in the Reference Example was added to replace an approximately equivalent amount of water (ODSO/Na (g/g)=6.67); other precursors are at ratios approximately equivalent to that in the Comparative Example 1, with a sol-gel SAR of about 30. Aluminum nitrate nonahydrate (0.6938 g) was weighed into a PTFE liner (45 ml). Thereafter, 0.8132 g of a 50 wt. % sodium hydroxide solution and 5.1084 g of a 40 wt. % TEAOH solution were added and the mixture stirred until the Al source dissolved. Next, distilled water (4.6674 g) and ODSO (1.5585 g) were added and the mixture was kept under stirring. The silica source (4.1705 g, Ludox AS-40, SiO₂ content of 40 wt. %) was added and the mixture stirred until homogeneous. The PTFE liner was positioned within an autoclave and transferred to an oven and heated to a temperature of 140° C. whilst rotating the autoclave. The autoclave was kept at isothermal conditions for 6 days. Thereafter, the product was filtered and washed with distilled water before drying at 110° C. The dry mass was 1.6196 g. The inorganic content determined by thermogravimetric (TGA) analysis was 86.2%, which corresponds to a zeolite yield of 1.3961 g. The as-made product was determined by x-ray diffraction to be mordenite zeolite, which was calcined at 550° C. (1° C./min ramp rate) for 8 hours to realize porous mordenite zeolite. The SAR (mol/mol) of the calcined mordenite zeolite was determined to be 24.4 by ICP spectroscopy.

Example 1E: ODSO as described in the Reference Example was added to replace an approximately equivalent amount of water (ODSO/Na (g/g)=7.97); other precursors are at ratios approximately equivalent to that in the Comparative Example 1, with a sol-gel SAR of about 30. Aluminum nitrate nonahydrate (0.6940 g) was weighed into a PTFE liner (45 ml). Thereafter, 0.8155 g of a 50 wt. % sodium hydroxide solution and 5.1048 g of a 40 wt. % TEAOH solution were added and the mixture stirred until the Al source dissolved. Next, distilled water (4.3561 g) and ODSO (1.8687 g) were added and the mixture was kept under stirring. The silica source (4.1699 g, Ludox AS-40, SiO₂ content of 40 wt. %) was added and the mixture stirred until homogeneous. The PTFE liner was positioned within an autoclave and transferred to an oven and heated to a temperature of 140° C. whilst rotating the autoclave. The autoclave was kept at isothermal conditions for 6 days. Thereafter, the product was filtered and washed with distilled water before drying at 110° C. The dry mass was 1.9797 g. The inorganic content determined by thermogravimetric (TGA) analysis was 80.3%, which corresponds to a zeolite yield of 1.5901 g. The as-made product was determined by x-ray diffraction to be co-crystallized mordenite/beta zeolite, which was calcined at 550° C. (1° C./min ramp rate) for 8 hours to realize porous co-crystallized mordenite/beta zeolite. The SAR (mol/mol) of the calcined co-crystallized zeolite was determined to be 27.8 by ICP spectroscopy.

Comparative Example 2: Precursors for synthesis of MFI zeolite, in particular ZSM-5, were provided in a comparative example, that is, in the absence of ODSO (ODSO/Na (g/g)=0), with a sol-gel SAR of about 100. Aluminum nitrate nonahydrate (0.2633 g) was weighed into a PTFE liner (45 ml). Thereafter, 0.7750 g of a 50 wt. % sodium hydroxide solution and 7.0469 g of a 20.1 wt % tetrapropylammonium hydroxide (TPAOH) solution were added and the mixture stirred. Next, distilled water (3.3005 g) was added and the mixture was maintained under stirring. Finally, the silica source (5.2430 g, Ludox AS-40, SiO₂ content of 40 wt. %) was added and the mixture stirred until homogeneous. The PTFE liner was positioned within an autoclave and transferred to an oven and heated to a temperature of 175° C. whilst rotating the autoclave. The autoclave was maintained at isothermal conditions for 18 hours. The product was filtered and washed with distilled water before drying at 110° C. The dry mass was 1.3906 g. The inorganic content determined by thermogravimetric (TGA) analysis was 87.78%, which corresponds to a product (zeolite) yield of 1.2207 g. The as-made product was determined by x-ray diffraction to be ZSM-5 zeolite, which was calcined at 550° C. (1° C./min ramp rate) for 8 hours to realize porous ZSM-5 zeolite. The SAR (mol/mol) of the ZSM-5 zeolite was determined to be 67.3 by ICP spectroscopy, and normalized to a value of 65.3.

Example 2A: ODSO as described in the Reference Example was added to replace an approximately equivalent amount of water (ODSO/Na (g/g)=5.31); other precursors are at ratios approximately equivalent to that in the Comparative Example 1, with a sol-gel SAR of about 100. Aluminum nitrate nonahydrate (0.2643 g) was weighed into a PTFE liner (45 ml). Thereafter, 0.7888 g of a 50 wt. % sodium hydroxide solution and 7.0383 g of a 20.1 wt % TPAOH solution were added and the mixture stirred. Next, distilled water (2.2038 g) and ODSO (1.2033 g) were added and the mixture was maintained under stirring. Finally, the silica source (5.2384 g, Ludox AS-40, SiO₂ content of 40 wt. %) was added and the mixture stirred until homogeneous. The PTFE liner was positioned within an autoclave and transferred to an oven and heated to a temperature of 175° C. whilst rotating the autoclave. The autoclave was maintained at isothermal conditions for 18 hours. The product was filtered and washed with distilled water before drying at 110° C. The dry mass was 2.1103 g. The inorganic content determined by thermogravimetric (TGA) analysis was 86.42%, which corresponds to a product (zeolite) yield of 1.8237 g. The as-made product was determined by x-ray diffraction to be ZSM-5 zeolite, which was calcined at 550° C. (1° C./min ramp rate) for 8 hours to realize porous ZSM-5 zeolite. The SAR (mol/mol) of the ZSM-5 zeolite was determined to be 97.2 by ICP spectroscopy, and normalized to a value of 94.4.

Example 2B: ODSO as described in the Reference Example was added to replace an approximately equivalent amount of water (ODSO/Na (g/g)=8.60); other precursors are at ratios approximately equivalent to that in the Comparative Example 1, with a sol-gel SAR of about 100. Aluminum nitrate nonahydrate (0.2605 g) was weighed into a PTFE liner (45 ml). Thereafter, 0.7435 g of a 50 wt. % sodium hydroxide solution and 7.0210 g of a 20.1 wt % TPAOH solution were added and the mixture stirred. Next, distilled water (1.4430 g) and ODSO (1.8384 g) were added and the mixture was maintained under stirring. Finally, the silica source (5.2235 g, Ludox AS-40, SiO₂ content of 40 wt. %) was added and the mixture stirred until homogeneous. The PTFE liner was positioned within an autoclave and transferred to an oven and heated to a temperature of 175° C. whilst rotating the autoclave. The autoclave was maintained at isothermal conditions for 18 hours. The product was filtered and washed with distilled water before drying at 110° C. The dry mass was 2.3550 g. The inorganic content determined by thermogravimetric (TGA) analysis was 88.05%, which corresponds to a product (zeolite) yield of 2.0736 g. The as-made product was determined by x-ray diffraction to be ZSM-5 zeolite, which was calcined at 550° C. (1° C./min ramp rate) for 8 hours to realize porous ZSM-5 zeolite. The SAR (mol/mol) of the ZSM-5 zeolite was determined to be 103.0 by ICP spectroscopy, and normalized to a value of 100.

Comparative Example 3: Precursors for synthesis of FAU zeolite, in particular Zeolite Y, were provided in a comparative example, that is, in the absence of ODSO (ODSO/Na (g/g)=0), with a sol-gel SAR of about 10. Aluminum isopropoxide (0.8677 g) was weighed into a PTFE liner (45 ml). Thereafter, 2.6679 g of a 50 wt. % sodium hydroxide was added and the mixture stirred. Next, distilled water (11.7746 g) was added and the mixture was maintained under stirring. Finally, the silica source (3.1256 g, Ludox AS-40, SiO₂ content of 40 wt. %) was added and the mixture stirred until homogeneous before ageing under stirring for 24 hrs. The PTFE liner was positioned within an autoclave and transferred to an oven and heated to a temperature of 100° C. whilst rotating the autoclave. The autoclave was maintained at isothermal conditions for 12 hours. The product was filtered, washed with distilled water and dried. The dry mass was 0.9083 g. The as-made product was determined by x-ray diffraction to be Zeolite Y (FAU). The SAR (mol/mol) of the (FAU) zeolite was determined to be 3.3 by ICP spectroscopy.

Example 3A: ODSO as described in the Reference Example was added to replace an approximately equivalent amount of water (ODSO/Na (g/g)=0.92); other precursors are at ratios approximately equivalent to that in the Comparative Example 3, with a sol-gel SAR of about 10. Aluminum isopropoxide (0.8676 g) was weighed into a PTFE liner (45 ml). Thereafter, 2.6662 g of a 50 wt. % sodium hydroxide was added and the mixture stirred. Next, distilled water (11.0680 g) and ODSO (0.7067 g) were added and the mixture was maintained under stirring. Finally, the silica source (3.1268 g, Ludox AS-40, SiO₂ content of 40 wt. %) was added and the mixture stirred until homogeneous before ageing under stirring for 24 hrs. The PTFE liner was positioned within an autoclave and transferred to an oven and heated to a temperature of 100° C. whilst rotating the autoclave. The autoclave was maintained at isothermal conditions for 12 hours. The product was filtered, washed with distilled water and dried. The dry mass was 0.9429 g. The as-made product was determined by x-ray diffraction to be Zeolite Y (FAU). The SAR (mol/mol) of the (FAU) zeolite was determined to be 3.6 by ICP spectroscopy.

Example 3B: ODSO as described in the Reference Example was added to replace an approximately equivalent amount of water (ODSO/Na (g/g)=1.85); other precursors are at ratios approximately equivalent to that in the Comparative Example 3, with a sol-gel SAR of about 10. Aluminum isopropoxide (0.8675 g) was weighed into a PTFE liner (45 ml). Thereafter, 2.6617 g of a 50 wt. % sodium hydroxide was added and the mixture stirred. Next, distilled water (10.3620 g) and ODSO (1.4133 g) were added and the mixture was maintained under stirring. Finally, the silica source (3.1269 g, Ludox AS-40, SiO₂ content of 40 wt. %) was added and the mixture stirred until homogeneous before ageing under stirring for 24 hrs. The PTFE liner was positioned within an autoclave and transferred to an oven and heated to a temperature of 100° C. whilst rotating the autoclave. The autoclave was maintained at isothermal conditions for 12 hours. The product was filtered, washed with distilled water and dried. The as-made product was determined by x-ray diffraction to be Zeolite Y (FAU). The SAR (mol/mol) of the (FAU) zeolite was determined to be 3.6 by ICP spectroscopy.

Table 2 shows these quantities, and the resulting SAR and product yields. It is clear that increasing the proportion of ODSO results in an increase in the SAR. Concomitantly, total zeolite yield is increased as a function of increasing ODSO content in the sol-gel. In certain embodiments, the SAR and/or the zeolite yield is increased, and zeolite having the same general zeolite framework as the equivalent water-only synthesis is produced, such as in Examples 1A (where *BEA zeolite is produced when the water-only synthesis also produced *BEA zeolite), 2A and 2B (where ZSM-5 zeolite is produced when the water-only synthesis also produced ZSM-5 zeolite) and 3A and 3B (where Zeolite Y (FAU) is produced when the water-only synthesis also produced Zeolite Y (FAU)). In certain embodiments, the SAR and/or the zeolite yield is increased, and zeolite having the same general zeolite framework as the equivalent water-only synthesis is produced along with one or more other types of zeolites and/or amorphous silica-alumina, such as in Example 1E (where co-crystallized *BEA/MOR zeolite is produced when the water-only synthesis also produced *BEA zeolite). In certain embodiments, the SAR and/or the zeolite yield is increased, and zeolite having a different general zeolite framework as the equivalent water-only synthesis is produced, such as in Examples 1B-1D (where MOR zeolite is produced when the water-only synthesis also produced *BEA zeolite).

As used herein, “approximately equivalent” as concerning the amount of ODSO that replaces water, the cumulative amount of ODSO and water, the component molar or mass ratios, and/or the hydrolysis conditions and time, is within a margin of less than or equal to plus or minus 1, 2, 5 or 10% of the compared value.

It is to be understood that like numerals in the drawings represent like elements through the several figures, and that not all components and/or steps described and illustrated with reference to the figures are required for all embodiments or arrangements. Further, the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the invention. As used herein, the singular forms “a”, “an” and “the” are intended to include the plural forms as well, unless the context clearly indicates otherwise. It will be further understood that the terms ““including,” “comprising,” or “having,” “containing,” “involving,” and variations thereof herein, when used in this specification, specify the presence of stated features, integers, steps, operations, elements, and/or components, but do not preclude the presence or addition of one or more other features, integers, steps, operations, elements, components, and/or groups thereof.

It should be noted that use of ordinal terms such as “first,” “second,” “third,” etc., in the claims to modify a claim element does not by itself connote any priority, precedence, or order of one claim element over another or the temporal order in which acts of a method are performed, but are used merely as labels to distinguish one claim element having a certain name from another element having a same name (but for use of the ordinal term) to distinguish the claim elements.

Notably, the figures and examples above are not meant to limit the scope of the present disclosure to a single implementation, as other implementations are possible by way of interchange of some or all the described or illustrated elements. Moreover, where certain elements of the present disclosure can be partially or fully implemented using known components, only those portions of such known components that are necessary for an understanding of the present disclosure are described, and detailed descriptions of other portions of such known components are omitted so as not to obscure the disclosure. In the present specification, an implementation showing a singular component should not necessarily be limited to other implementations including a plurality of the same component, and vice-versa, unless explicitly stated otherwise herein. Moreover, applicants do not intend for any term in the specification or claims to be ascribed an uncommon or special meaning unless explicitly set forth as such. Further, the present disclosure encompasses present and future known equivalents to the known components referred to herein by way of illustration.

The foregoing description of the specific implementations will so fully reveal the general nature of the disclosure that others can, by applying knowledge within the skill of the relevant art(s), readily modify and/or adapt for various applications such specific implementations, without undue experimentation, without departing from the general concept of the present disclosure. Such adaptations and modifications are therefore intended to be within the meaning and range of equivalents of the disclosed implementations, based on the teaching and guidance presented herein. It is to be understood that the phraseology or terminology herein is for the purpose of description and not of limitation, such that the terminology or phraseology of the present specification is to be interpreted by the skilled artisan in light of the teachings and guidance presented herein, in combination with the knowledge of one skilled in the relevant art(s). It is to be understood that dimensions discussed or shown are drawings accordingly to one example and other dimensions can be used without departing from the disclosure.

The subject matter described above is provided by way of illustration only and should not be construed as limiting. Various modifications and changes can be made to the subject matter described herein without following the example embodiments and applications illustrated and described, and without departing from the true spirit and scope of the invention encompassed by the present disclosure, which is defined by the set of recitations in the following claims and by structures and functions or steps which are equivalent to these recitations.

TABLE 1 ODSO Name Formula Structure Examples Dialkyl-sulfonesulfoxide Or 1,2-alkyl-alkyl-disulfane 1,1,2-trioxide (R-SOO-SO-R′)

Dialkyl-disulfone Or 1,2 alkyl-alkyl-disulfane 1,1,2,2-tetraoxide (R-SOO-SOO-R′)

Alkyl-sulfoxidesulfonate (R-SO-SOO-OH)

Alkyl-sulfonesulfonate (R-SOO-SOO-OH)

Alkyl-sulfoxidesulfinate (R-SO-SO-OH)

Alkyl-sulfonesulfinate (R-SOO-SO-OH)

R and R′ can be the same or different alkyl or aryl groups comrpising 1-10 carbon atoms.

TABLE 2 SAR Yield increase Zeolite increase ODSO/Na SAR (relative to Yield (relative to Example Framework (g/g) (mol/mol) comparative) (g) comparative) Comp. 1 *BEA 0.0 16.3 — 0.9119 — 1A *BEA 1.33 17.8 9.2% 1.0366 13.7% 1B MOR 2.66 18.6 14.1% 1.0471 14.5% 1C MOR 3.99 20.2 22.7% 1.1182 22.6% 1D MOR 6.67 24.4 49.7% 1.3962 53.1% 1E *BEA/MOR 7.97 27.8 70.6% 1.5901 74.3% Comp. 2 ZSM-5 0.0 65.3 — 1.2207 — 2A ZSM-5 5.3 94.4 44.6% 1.8237 49.4% 2B ZSM-5 8.6 100 53.2% 2.0736 69.9% Comp. 3 FAU 0.0 3.3 — 0.9083 — 3A FAU 0.92 3.6 9.1% 0.9429 3.8% 3B FAU 1.85 3.6 9.1% — — Note that some values were not measured and indicated with a dash in Table 2. 

1. A method for synthesis of zeolite comprising: forming a homogeneous aqueous mixture of a silica source, an aluminum source, an alkali metal source, water and water-soluble oxidized disulfide oil (ODSO); and heating the homogeneous aqueous mixture under conditions and for a time effective to form a crystalline zeolite as precipitate suspended in a supernatant, wherein the zeolite is characterized by a silica-to-alumina ratio that is greater than that of a comparative material, and wherein the comparative material is formed of approximately equivalent composition of components except for water instead of the added ODSO, and under approximately equivalent conditions and time.
 2. The method of claim 1, wherein an increase in a sub-ratio of water-soluble ODSO to water effects an increase in the silica-to-alumina ratio.
 3. The method of claim 1, wherein the zeolite is characterized by a zeolite yield, and wherein the zeolite yield is greater than that of the comparative material.
 4. The method of claim 3, wherein an increase in a sub-ratio of water-soluble ODSO to water effects an increase in the zeolite yield.
 5. The method as in claim 1, wherein the homogeneous aqueous mixture has a pH in the range of about 9-14, and wherein an increase in a sub-ratio of water-soluble ODSO to water effects a decrease in pH.
 6. The method as in claim 1, wherein the alkali metal source is sodium and the mass ratio of ODSO to sodium is in the range of about 0.1-10.
 7. The method as in claim 1, wherein the ODSO is derived from oxidation of disulfide oil compounds present in an effluent refinery hydrocarbon stream recovered following catalytic oxidation of mercaptans present in a mercaptan-containing hydrocarbon stream.
 8. The method as in claim 1, wherein the ODSO compounds have 3 or more oxygen atoms and include one or more compounds selected from the group consisting of (R—SOO—SO—R′), (R—SOO—SOO—R′), (R—SO—SOO—OH), (R—SOO—SOO—OH), (R—SOO—SO—OH), (X—SO—OR) and (X—SOO—OR), wherein R and R′ are alkyl or aryl groups comprising 1-10 carbon atoms and wherein X denotes esters and is (R—SO) or (R—SOO).
 9. The method as in claim 1, wherein the ODSO compounds have 3 or more oxygen atoms and include two or more compounds selected from the group consisting of (R—SOO—SO—R′), (R—SOO—SOO—R′), (R—SO—SOO—OH), (R—SOO—SOO—OH), (R—SOO—SO—OH), (X—SO—OR) and (X—SOO—OR), wherein R and R′ are alkyl or aryl groups comprising 1-10 carbon atoms and wherein X denotes esters and is (R—SO) or (R—SOO).
 10. The method as in claim 1, wherein the ODSO compounds have 3 or more oxygen atoms and include one or more compounds selected from the group consisting of (R—SOO—SO—R′), (R—SOO—SOO—R′), (R—SO—SOO—OH), (R—SOO—SOO—OH), (R—SO—SO—OH), (R—SOO—SO—OH), wherein R and R′ are alkyl or aryl groups comprising 1-10 carbon atoms.
 11. The method as in claim 1, wherein the aluminum source comprises aluminates, alumina, other zeolites, aluminum colloids, boehmites, pseudo-boehmites, aluminum hydroxides, aluminum salts, aluminum alkoxides, aluminum wire or alumina gels.
 12. The method as in claim 1, wherein the silica source comprises sodium silicate (water glass), rice husk, fumed silica, precipitated silica, colloidal silica, silica gels, zeolites, dealuminated zeolites, silicon hydroxides or silicon alkoxides.
 13. The method as in claim 1, wherein crystallization occurs in the absence of a seed.
 14. The method as in claim 1, wherein crystallization occurs in the presence of a seed.
 15. The method as in claim 1, wherein the homogeneous aqueous mixture further comprises a structure directing agent that is selected to influence the type of zeolite produced.
 16. A method for synthesis of a first zeolite material and a second zeolite material comprising: forming a first homogeneous aqueous mixture at a first ratio of a silica source, an aluminum source, an alkali metal source, water, an optional a structure directing agent, and water-soluble oxidized disulfide oil (ODSO); heating the first homogeneous aqueous mixture under conditions and for a time effective to form a first crystalline zeolite as a first precipitate suspended in a supernatant, wherein the first zeolite material is characterized by a first silica-to-alumina ratio; forming a second homogeneous aqueous mixture at a second ratio of a silica source, an aluminum source, an alkali metal source, water, an optional a structure directing agent, and water-soluble ODSO, wherein the second ratio is approximately the same as the first ratio except for a ratio of water and water-soluble ODSO in the solution, wherein an amount of ODSO in the second homogeneous aqueous mixture is greater than an amount of ODSO in the first homogeneous aqueous mixture; heating the second homogeneous aqueous mixture approximately equivalent conditions and time as compared to the heating of the first homogeneous aqueous mixture to form a second crystalline zeolite as a second precipitate suspended in a supernatant, wherein the second zeolite material is characterized by a second silica-to-alumina ratio, and wherein the second silica-to-alumina ratio is greater than the first silica-to-alumina ratio.
 17. The method of claim 16, wherein the first zeolite material and the second zeolite material zeolite are characterized by a first zeolite yield and a second zeolite yield, and wherein the second zeolite yield is greater than the first zeolite yield. 